Process of converting oils



. `Tan. I9, 1932. A. P. sAcHs PROCESS OF CONVERTING OILS Filed April 17, 1928 vPatented Jan. 19, 1932 -take place in one stage only) withone- Um'rlazu` STATES PATE NT` OFFICE ALBERT I. SACHS, OF NEW YORK, N. Y ASSIGNOR T0 PETROLEUM CONVERSION OOR- IORATION, OF NEW YORK, NQY.,

A CORPORATION OF DELAWARE raocnss or cammina omsx Application ma april 17,

`system of conversion to which myy invention is particularly adapted, the conversion is broughtl about in the va or phase, the oil material being previous y vaporized and then mingled with a gaseous carrier usually of hydrocarbon origin, which is heated to the proper temperature and is of suicient quantity to carry out the desired reaction.

The present invention is particularly concerned with the manner of lapplying' the arrier gas to the body. of vapor undergoing conversion whereby a more eilicient heating of the oil va ors 1s obtained. Prior to, my discovery itA as been the practice to mingle the carrier gas and va 'or to be converted in one operation, a su cientl long-path for the mixture being provided1 to give the necessary time for cracking. I have now discovered th'ata more eiliclent mixing and heating will be had by mingling the carrier gas in stages whereby the vapor to be cracked is maintalned overgiglonger courseat a higher average temperature. In other words the temperature of the vapors undergoing cracking 1s raised as soon as such temperature has 1 dropped a predetermined amount, thus maintaining a more uniform temperatureover a longer time interval and producing a greater yield of the cracked material sought.

According to one method of carrying out my invention, I mingle one-half the quantity ofoil vapor (with reference to the' amount which would have been used with a given `quantity of carrier gas were the to alf the available carrier gas in. one stage, then at a second stage in the travel of the mixture,

- I introduce an additional quarter of the carrier gas, and finally at a third point, the remaming quarter of the carrier gas is introduced. Preferably, though not necessarily, a separate chamberis provided for each stage. In this manner, while a less quantity of oil vapor is treated per cubic foot of car- 192s. serial nu. aman.`

rier gas, the average temperature to which exit temperature of the products is had, a

greater amount of heat is available for transfer to other products destined for the reac-f tion chambers 'so 'that a substantial portion of this additionalheat is recovered.

In the accompanying drawing, I have il` lustr'ated more or less diagrammatically, an

apparatus for carrying out the invention as described in the foregoing.

In said drawing, reactionl chamber No.1 is supplied with vapor from a still 10 through a pipe 11 having a control valve 12, such vapor preferably having been produced in said still without havin undergone xan appreciable amount of crardng. Also supplied to reaction chamber 1 through a main B is a carrier gas of the desired temperature, and in sufficient amount to provide the desired number of heat units from a heating element 14 preferably in the form (if a regenerative heater or hot blaststove, the gas having been passed therethroughlfr'om alholder 15. For sake of example'the temperature of the carrler gas may be taken as 1400 degrees and'that of the oil vapor 650 degrees F. the temperature being regulated by, means of valve 15a in the oil'take to chamber No.1. The oil vapor coming in contact with the heated gaseous car'- rier is raised in temperature to say 1050 degrecs F. which mayy be taken as a desirable upper limit of the conversion range,l the exit temperature from the first reaction chamber being in the neighborhood of 990 degrees F.I The products from reaction chamber No. 1 are now by means of pipe 16 brought into reaction chamber No 2 wherein a further quantity of carrier gas controlled by valve 16a is introduced equal, preferably, to one-half the remainder or one-quarter of the total quantity of gaseous carrier, this having the effect of raising vthe temperature of the `products of from say 990 degrees F. to 1030 degrees F.

The mixture passing out of the second reaction chamber is conducted through pipe 17 to a third .reaction chamber No. 3, where1n the mixture is subjected to the remaining quarter of the carrier gas from the stove 14 and introduced through valve 17 a. In this cham- .ber the temperature of the gases which may have fallen to around 970 degrees is raised to 1035 degrees, the exit temperature of the gases from reaction chamber No. 3 being say in the neighborhood of 975 degrees.

The inal mixture leaving reaction chamber 3 may now be passed through a pipe 20 to the usual heat exchangers, rectifying and condensing columns in the last of which' the gasoline-like products are recovered. Since the above-mentioned elements form no part of the present invention they have not been illustrated.

lt will be understood that the temperatures different stages and the number of the latter may be varied as desired. Furthermore it is not imperative that separate chambers be employed at each stage so long as the proper time element is allowed therefor and provided that means are afforded for the partially cooled reaction mixture to be properly mixed with the additional reheating gas which may be introduced at any point in the travel of the reacting mixture.

at l claim is:

1. ln the process of converting oils in the vaporphase by mingling the oil vapor with a heated carrier gas of such quantity and temperature as to bring about the conversion reaction, the steps which consists in rst subjecting the oil to be converted to vaporizing conditions in a vaporizing zone, separating the produced vapor from the unvaporized liquid, adding in stages in a reaction zone Asuch carrier gas to oil vapor derived from said va; porizing zone and so proportioning the gas to the vapor in the first stage as to raise the. temperature of said vapor to substantially` that of the desired conversion temperature in excess of 900 F., allowing said reaction to take place over an applicable time interval,

l then adding in a second stage but before the temperature of the reacting mixture has dropped a predetermined amount, a furtherl quantity of said carrier gas at substantially the same temperature as that added in said first stage and in sufficient quantity to raise 1 the temperature of said mixture t0 substan tially said original reaction temperature.

mentioned is not substantially greater than 100 F., and in'which moreL than two stages are provided, approximately one-half the total quantity of carrier gasvbeing added in the first stage and the remainder of said gas divided substantially equally among the remaining stages.

4. The process according to claim 1, in which the initial temperature of the gas and vapor mixture is approximately 1000 F., and in which the temperature drop mentioned is not substantially greater than 100 F.

ln testimony whereof I have affixed my signature to this specification.

ALBERT P. SACHS.

2. The process according to the preceding claim, in which the predetermined temperature drop mentioned is not substantially greater than 100 F. L

3. The process according to claim 1, in which the predetermined temperature drop ina` CERTIFICATE OF CORRECTION.

' Patent No. 1,842,321.. y January 19, 1932.

ALBERT P. sAens.

f It is hereby certified that error appears in the printed specification of the above numbered patent requiring correction as follows:v Page 2, line 51, claim l, for "applcable read appreciable; and that the said Letters Patent should be read with this correction therein that the same may conform to the record of the case in the Patent Office. a

Signed and sealedthis 29th day of November, iA. D. 1932.

t. M. J.

(Seal) Acting Commissioner of Patents. 

